Natural gas liquid fractionation plant waste heat conversion to cooling capacity using kalina cycle

ABSTRACT

Certain aspects of natural gas liquid fractionation plant waste heat conversion to cooling capacity using Kalina Cycle can be implemented as a system, which includes a waste heat recovery heat exchanger to heat a buffer fluid stream by exchange with a heat source in a natural gas liquid fractionation plant. The system includes a Kalina cycle energy conversion system including one or more first energy conversion heat exchangers to heat a first portion of a working fluid by exchange with the heated buffer fluid stream, a separator to receive the heated working fluid and to output a vapor stream of the working fluid and the liquid stream of the working fluid, and a cooling subsystem including a first cooling element to condense the vapor stream of the working fluid and a second cooling element configured to cool a process fluid stream from the natural gas liquid fractionation plant by exchange with the condensed vapor stream of the working fluid.

CROSS-REFERENCE TO RELATED APPLICATIONS

This disclosure claims the benefit of priority to U.S. Application Ser. No. 62/542,687 entitled “Utilizing Waste Heat Recovered From Natural Gas Liquid Fractionation Plants”, which was filed on Aug. 8, 2017, the entire contents of which are incorporated herein by reference.

TECHNICAL FIELD

This disclosure relates to operating industrial facilities, for example, a natural gas liquid fractionation plant or other industrial facilities that include operating plants that generate heat, for example, a natural gas liquid fractionation plant.

BACKGROUND

Natural gas liquid (NGL) processes are chemical engineering processes and other facilities used in petroleum refineries to transform natural gas into products, for example, liquefied petroleum gas (LPG), gasoline, kerosene, jet fuel, diesel oils, fuel oils, and such products. NGL facilities are large industrial complexes that involve many different processing units and auxiliary facilities, for example, utility units, storage tanks, and such auxiliary facilities. Each refinery can have its own unique arrangement and combination of refining processes determined, for example, by the refinery location, desired products, economic considerations, or such factors. The NGL processes that are implemented to transform the natural gas into the products such as those listed earlier can generate heat, which may not be reused, and byproducts, for example, greenhouse gases (GHG), which may pollute the atmosphere. It is believed that the world's environment has been negatively affected by global warming caused, in part, due to the release of GHG into the atmosphere.

SUMMARY

This specification describes technologies relating to cooling capacity generation, power generation or potable water production from waste heat in a natural gas liquid (NGL) fractionation plant.

The present disclosure includes one or more of the following units of measure with their corresponding abbreviations, as shown in Table 1:

TABLE 1 Unit of Measure Abbreviation Degrees Celsius ° C. Megawatts MW One million MM British thermal unit Btu Hour h Pounds per square inch (pressure) psi Kilogram (mass) Kg Second S Cubic meters per day m³/day Fahrenheit F.

An example implementation includes a system. The system includes a waste heat recovery heat exchanger configured to heat a buffer fluid stream by exchange with a heat source in a natural gas liquid fractionation plant. The system includes a Kalina cycle energy conversion system including one or more first energy conversion heat exchangers configured to heat a first portion of a working fluid by exchange with the heated buffer fluid stream, a separator configured to receive the heated working fluid and to output a vapor stream of the working fluid and the liquid stream of the working fluid, and a cooling subsystem including a first cooling element configured to condense the vapor stream of the working fluid and a second cooling element configured to cool a process fluid stream from the natural gas liquid fractionation plant by exchange with the condensed vapor stream of the working fluid.

In an aspect combinable with the example implementation, the cooling subsystem is configured to produce at least 350 MM Btu/h of cooling capacity for the natural gas liquid fractionation plant. In another aspect combinable with any of the previous aspects, the second cooling element is configured to cool ethane gas output from a deethanizer in the natural gas liquid fractionation plant. In another aspect combinable with any of the previous aspects, the second cooling element comprises a chiller having a thermal duty of between 300 MM Btu/h and 500 MM Btu/h. In another aspect combinable with any of the previous aspects, the first cooling element comprises a cooler having a thermal duty of between 400 Btu/h and 600 Btu/h. In another aspect combinable with any of the previous aspects, the first cooling element comprises a valve. In another aspect combinable with any of the previous aspects, the valve is configured to condense the working fluid to a pressure of between 4 Bar and 5 Bar and a temperature of between 30° F. and 50° F. In another aspect combinable with any of the previous aspects, the energy conversion system comprises a pump configured to pump the working fluid to a pressure of between 11 Bar and 12 Bar. In another aspect combinable with any of the previous aspects, the one or more first energy conversion heat exchangers include an energy conversion heat exchanger having a thermal duty of between 100 MM Btu/h and 200 MM Btu/h, and an energy conversion heat exchanger having a thermal duty of between 400 MM Btu/h and about 500 MM Btu/h. In another aspect combinable with any of the previous aspects, the one or more first energy conversion heat exchangers are configured to heat the first portion of the working fluid to a temperature of between 160° F. and 180° F. In another aspect combinable with any of the previous aspects, the one or more first energy conversion heat exchangers are configured to heat a first portion of the working fluid. In another aspect combinable with any of the previous aspects, the Kalina cycle energy conversion system includes one or more second energy conversion heat exchangers configured to heat a second portion of the working fluid, the second by exchange with the liquid stream of the working fluid. In another aspect combinable with any of the previous aspects, the separator is configured to receive the heated first and second portions of the working fluid. In another aspect combinable with any of the previous aspects, the one or more second energy conversion heat exchangers are configured to heat the second portion of the working fluid by exchange with the heated buffer fluid stream. In another aspect combinable with any of the previous aspects, the one or more second energy conversion heat exchangers include a heat exchanger having a thermal duty of between 150 MM Btu/h and 250 MM Btu/h, and a heat exchanger having a thermal duty of between 300 MM Btu/h and about 400 MM Btu/h. In another aspect combinable with any of the previous aspects, the one or more second energy conversion heat exchangers are configured to heat the second portion of the working fluid to a temperature of between 160° F. and 180° F. In another aspect combinable with any of the previous aspects, the system includes a turbine configured to generate power from the liquid stream of the working fluid. In another aspect combinable with any of the previous aspects, the second turbine is configured to generate at least 0.1 MW of power. In another aspect combinable with any of the previous aspects, the second turbine includes a high pressure recovery turbine. In another aspect combinable with any of the previous aspects, the system includes a storage tank. In another aspect combinable with any of the previous aspects, the buffer fluid stream flows from the storage tank, through the waste heat recovery heat exchanger, through the Kalina cycle energy conversion system, and back to the storage tank. In another aspect combinable with any of the previous aspects, the waste heat recovery heat exchanger is configured to heat the buffer fluid stream by exchange with propane gas output from a propane dehydrator in the natural gas liquid fractionation plant. In another aspect combinable with any of the previous aspects, the waste heat recovery heat exchanger is configured to heat the buffer fluid stream by exchange with a C5+ bottoms product from a debutanizer in the natural gas liquid fractionation plant. In another aspect combinable with any of the previous aspects, the waste heat recovery heat exchanger is configured to heat the buffer fluid stream by exchange with butane gas output from a debutanizer in the natural gas liquid fractionation plant. In another aspect combinable with any of the previous aspects, the waste heat recovery heat exchanger is configured to heat the buffer fluid stream by exchange with butane gas output from a butane dehydrator in the natural gas liquid fractionation plant. In another aspect combinable with any of the previous aspects, the waste heat recovery heat exchanger is configured to heat the buffer fluid stream by exchange with pentane gas output from a depentanizer in the natural gas liquid fractionation plant. In another aspect combinable with any of the previous aspects, the waste heat recovery exchanger is configured to heat the buffer fluid stream by exchange with acid gases output from an ADIP generator in the natural gas liquid fractionation plant. In another aspect combinable with any of the previous aspects, the waste heat recovery exchanger is configured to heat the buffer fluid stream by exchange with lean ADIP output from an ADIP generator in the natural gas liquid fractionation plant. In another aspect combinable with any of the previous aspects, the waste heat recovery exchanger is configured to heat the buffer fluid stream by exchange with light NG components output from a pre-flash drum in a decolorizing section of the natural gas liquid fractionation plant. In another aspect combinable with any of the previous aspects, the waste heat recovery exchanger is configured to heat the buffer fluid stream by exchange with NG gas output from a decolorizer in the natural gas liquid fractionation plant. In another aspect combinable with any of the previous aspects, the waste heat recovery exchanger is configured to heat the buffer fluid stream by exchange with compressed propane in the natural gas liquid fractionation plant. In another aspect combinable with any of the previous aspects, the waste heat recovery exchanger is configured to heat the buffer fluid stream by exchange with dry ethane gas in the natural gas liquid fractionation plant. In another aspect combinable with any of the previous aspects, the waste heat recovery exchanger is configured to heat the buffer fluid stream by exchange with pentane gas output from an RVP column in the natural gas liquid fractionation plant.

An example implementation includes a method. A buffer fluid stream is heated via a waste heat recovery heat exchanger by exchange with a heat source in a natural gas liquid fractionation plant. Power is generated in a Kalina cycle energy conversion system by heating a working fluid via one or more first energy conversion heat exchangers by exchange with the heated buffer fluid stream, separating, in a separator, the heated working fluid into a vapor stream of the working fluid and the liquid stream of the working fluid, condensing the vapor stream of the working fluid, and cooling a process fluid stream in the natural gas liquid fractionation plant by exchange with the condensed vapor stream of the working fluid.

This, and other aspects, can include one or more of the following features. In another aspect combinable with any of the previous aspects, the cooling subsystem is configured to produce at least 350 MM Btu/h of cooling capacity for the natural gas liquid fractionation plant. In another aspect combinable with any of the previous aspects, the second cooling element is configured to cool ethane gas output from a deethanizer in the natural gas liquid fractionation plant. In another aspect combinable with any of the previous aspects, the second cooling element comprises a chiller having a thermal duty of between 300 MM Btu/h and 500 MM Btu/h. In another aspect combinable with any of the previous aspects, the first cooling element comprises a cooler having a thermal duty of between 400 Btu/h and 600 Btu/h. In another aspect combinable with any of the previous aspects, the first cooling element comprises a valve. In another aspect combinable with any of the previous aspects, the valve is configured to condense the working fluid to a pressure of between 4 Bar and 5 Bar and a temperature of between 30° F. and 50° F. In another aspect combinable with any of the previous aspects, the energy conversion system comprises a pump configured to pump the working fluid to a pressure of between 11 Bar and 12 Bar. In another aspect combinable with any of the previous aspects, the one or more first energy conversion heat exchangers include an energy conversion heat exchanger having a thermal duty of between 100 MM Btu/h and 200 MM Btu/h, and an energy conversion heat exchanger having a thermal duty of between 400 MM Btu/h and about 500 MM Btu/h. In another aspect combinable with any of the previous aspects, the one or more first energy conversion heat exchangers are configured to heat the first portion of the working fluid to a temperature of between 160° F. and 180° F. In another aspect combinable with any of the previous aspects, the one or more first energy conversion heat exchangers are configured to heat a first portion of the working fluid. In another aspect combinable with any of the previous aspects, the Kalina cycle energy conversion system includes one or more second energy conversion heat exchangers configured to heat a second portion of the working fluid, the second by exchange with the liquid stream of the working fluid. In another aspect combinable with any of the previous aspects, the separator is configured to receive the heated first and second portions of the working fluid. In another aspect combinable with any of the previous aspects, the one or more second energy conversion heat exchangers are configured to heat the second portion of the working fluid by exchange with the heated buffer fluid stream. In another aspect combinable with any of the previous aspects, the one or more second energy conversion heat exchangers include a heat exchanger having a thermal duty of between 150 MM Btu/h and 250 MM Btu/h, and a heat exchanger having a thermal duty of between 300 MM Btu/h and about 400 MM Btu/h. In another aspect combinable with any of the previous aspects, the one or more second energy conversion heat exchangers are configured to heat the second portion of the working fluid to a temperature of between 160° F. and 180° F. In another aspect combinable with any of the previous aspects, the system includes a turbine configured to generate power from the liquid stream of the working fluid. In another aspect combinable with any of the previous aspects, the second turbine is configured to generate at least 0.1 MW of power. In another aspect combinable with any of the previous aspects, the second turbine includes a high pressure recovery turbine. In another aspect combinable with any of the previous aspects, the system includes a storage tank. In another aspect combinable with any of the previous aspects, the buffer fluid stream flows from the storage tank, through the waste heat recovery heat exchanger, through the Kalina cycle energy conversion system, and back to the storage tank. In another aspect combinable with any of the previous aspects, the waste heat recovery heat exchanger is configured to heat the buffer fluid stream by exchange with propane gas output from a propane dehydrator in the natural gas liquid fractionation plant. In another aspect combinable with any of the previous aspects, the waste heat recovery heat exchanger is configured to heat the buffer fluid stream by exchange with a C5+ bottoms product from a debutanizer in the natural gas liquid fractionation plant. In another aspect combinable with any of the previous aspects, the waste heat recovery heat exchanger is configured to heat the buffer fluid stream by exchange with butane gas output from a debutanizer in the natural gas liquid fractionation plant. In another aspect combinable with any of the previous aspects, the waste heat recovery heat exchanger is configured to heat the buffer fluid stream by exchange with butane gas output from a butane dehydrator in the natural gas liquid fractionation plant. In another aspect combinable with any of the previous aspects, the waste heat recovery heat exchanger is configured to heat the buffer fluid stream by exchange with pentane gas output from a depentanizer in the natural gas liquid fractionation plant. In another aspect combinable with any of the previous aspects, the waste heat recovery exchanger is configured to heat the buffer fluid stream by exchange with acid gases output from an ADIP generator in the natural gas liquid fractionation plant. In another aspect combinable with any of the previous aspects, the waste heat recovery exchanger is configured to heat the buffer fluid stream by exchange with lean ADIP output from an ADIP generator in the natural gas liquid fractionation plant. In another aspect combinable with any of the previous aspects, the waste heat recovery exchanger is configured to heat the buffer fluid stream by exchange with light NG components output from a pre-flash drum in a decolorizing section of the natural gas liquid fractionation plant. In another aspect combinable with any of the previous aspects, the waste heat recovery exchanger is configured to heat the buffer fluid stream by exchange with NG gas output from a decolorizer in the natural gas liquid fractionation plant. In another aspect combinable with any of the previous aspects, the waste heat recovery exchanger is configured to heat the buffer fluid stream by exchange with compressed propane in the natural gas liquid fractionation plant. In another aspect combinable with any of the previous aspects, the waste heat recovery exchanger is configured to heat the buffer fluid stream by exchange with dry ethane gas in the natural gas liquid fractionation plant. In another aspect combinable with any of the previous aspects, the waste heat recovery exchanger is configured to heat the buffer fluid stream by exchange with pentane gas output from an RVP column in the natural gas liquid fractionation plant.

The details of one or more implementations of the subject matter described in this specification are set forth in the accompanying drawings and the detailed description. Other features, aspects, and advantages of the subject matter will become apparent from the description, the drawings, and the claims.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1A is a diagram of a low grade waste heat recovery system.

FIG. 1B is a diagram of a Kalina cycle based waste heat to cooling conversion plant.

FIG. 1C is a diagram of a propane dehydrator section of a NGL fractionation plant.

FIG. 1D is a diagram of a debutanizer section of a NGL fractionation plant.

FIG. 1E is a diagram of a butane dehydrator section of a NGL fractionation plant.

FIG. 1F is a diagram of a depentanizer section of a NGL fractionation plant.

FIG. 1G is a diagram of a solvent regeneration section of a NGL fractionation plant.

FIG. 1H is a diagram of a natural gasoline decolorizing section of a NGL fractionation plant.

FIG. 1I is a diagram of a propane tank recovery section of a NGL fractionation plant.

FIG. 1J is a diagram of a propane product refrigeration section of a NGL fractionation plant.

FIG. 1K is a diagram of a propane product sub-cooling section of a NGL fractionation plant.

FIG. 1L is a diagram of an ethane production section of a NGL fractionation plant.

FIG. 1M is a diagram of a natural gasoline vapor section.

DETAILED DESCRIPTION

NGL Plant

Gas processing plants can purify raw natural gas or crude oil production associated gases (or both) by removing common contaminants such as water, carbon dioxide and hydrogen sulfide. Some of the substances which contaminate natural gas have economic value and can be processed or sold or both. Upon the separation of methane gas, which is useful as sales gas for houses and power generation, the remaining hydrocarbon mixture in liquid phase is called natural gas liquids (NGL). The NGL is fractionated in a separate plant or sometimes in the same gas processing plant into ethane, propane and heavier hydrocarbons for several versatile uses in chemical and petrochemical as well as transportation industries. The NGL fractionation plant uses the following processes or sections: fractionation, product treating, and natural gasoline processing. The fractionation processes or sections can include heat sources (also commonly referred to as streams) including, but not limited to, a propane condenser, a propane refrigerant condenser, a naphtha cooler, a de-pentanizer condenser, an amine-di-iso-propanol (ADIP) cooler, a regenerator overhead (OVHD) condenser, a Reid vapor pressure (RVP) column condenser, a de-propanizer condenser, a de-butanizer condenser, or combinations thereof. The product treating processes or sections can include the following non-limiting heat sources: a propane dehydrator condenser, a butane dehydrator condenser, a propane condenser, an air-cooled condenser, a regeneration gas cooler, and a butane condenser, or combinations thereof. The natural gasoline processing processes or sections can include, but are not limited to, a natural gasoline (NG) flash vapor condenser, a NG de-colorizer condenser, or combinations thereof.

Fractionation Section

Fractionation is the process of separating the different components of natural gas. Separation is possible because each component has a different boiling point. At temperatures less than the boiling point of a particular component, that component condenses to a liquid. It is also possible to increase the boiling point of a component by increasing the pressure. By using columns operating at different pressures and temperatures, the NGL fractionation plant is capable of separating ethane, propane, butane, pentane, or combinations thereof (with or without heavier associated hydrocarbons) from NGL fractionation feeds. De-ethanizing separates ethane from C2+ NGL, where C2 refers to a molecule containing two carbon atoms (ethane), and where C2+ refers to a mixture containing molecules having two or more carbon atoms, for example, a NGL containing C2, C3, C4, C5 can be abbreviated as “C2+ NGL”. De-propanizing and de-butanizing separate propane and butane, respectively, from C3+ NGL and C4+ NGL, respectively. Because the boiling points of heavier natural gases are closer to each other, such gases can be harder to separate compared to lighter natural gases. Also, a rate of separation of heavier components is less than that of comparatively lighter components. In some instances, the NGL fractionation plant can implement, for example, about 45 distillation trays in the de-ethanizer, about 50 trays in the de-propanizer, and about 55 trays in the de-butanizer.

The fractionation section can receive a feed gas containing C2+ NGL from gas plants, which are upstream plants that condition and sweeten the feed gas, and produce a sales gas, such as a C1/C2 mixture, where C1 is about 90%, as a final product. The C2+ NGL from gas plants can be further processed in the NGL fractionation plant for C2+ recovery. From feed metering or surge unit metering (or both), feed flows to the three fractionation modules, namely, the de-ethanizing module, the de-propanizing module and the de-butanizing module, each of which is described later.

De-Ethanizer Module (or De-Ethanizer Column)

The C2+ NGL is pre-heated before entering the de-ethanizer column for fractionation. The separated ethane leaves the column as overhead gas. The ethane gas is condensed by a closed-loop propane refrigeration system. After being cooled and condensed, the ethane is a mixture of gas and liquid. The liquid ethane is separated and pumped back to the top of the column as reflux. The ethane gas is warmed in an economizer and then sent to users. The bottoms product from the de-ethanizer reboiler is C3+ NGL, which is sent to the de-propanizer module.

De-Propanizer Module (or De-Propanizer Column)

From the de-ethanizer module, C3+ NGL enters the de-propanizer module for fractionation. The separated propane leaves the column as overhead gas. The gas is condensed using coolers. The propane condensate is collected in a reflux drum. Some of the liquid propane is pumped back to the column as reflux. The rest of the propane is either treated or sent to users as untreated product. The bottoms product from the depropanizer reboiler, C4+ is then sent to the de-butanizer module

De-Butanizer Module (or De-Butanizer Column)

C4+ enters the de-butanizer module for fractionation. The separated butane leaves the column as overhead gas. The gas is condensed using coolers. The butane condensate is collected in a reflux drum. Some of the liquid butane is pumped back to the column as reflux. The rest of the butane is either treated or sent to users as untreated product. The bottoms product from the debutanizer reboiler, C5+ natural gas (NG) goes on to a RVP control section (which may also be referred to as a rerun unit), which will be discussed in greater detail in a later section.

Product Treating Section

While ethane requires no further treatment, propane and butane products are normally treated to remove hydrogen sulfide (H₂S), carbonyl sulfide (COS), and mercaptan sulfur (RSH). Then, the products are dried to remove any water. All exported product is treated, while untreated products can go to other industries. As described later, propane receives ADIP treating, MEROX™ (Honeywell UOP; Des Plaines, Ill.) treating, and dehydration. Butane receives MEROX treating, and dehydration.

ADIP Treating Section

ADIP is a solution of di-isopropanol amine and water. ADIP treating extracts H₂S and COS from propane. The ADIP solution, through contact with the sour propane, absorbs the H₂S and COS. The ADIP solution first contacts the sour propane in an extractor. In the extractor, the ADIP absorbs most of the H₂S and some of the COS. The propane then passes through a mixer/settler train where the propane contacts with ADIP solution to extract more H₂S and COS. This partially sweetened propane is cooled and then washed with water to recover the ADIP entrained with the propane. The propane is then sent to MEROX treating, which is described later. The rich ADIP that has absorbed the H₂S and COS leaves the bottom of the extractor and is regenerated into lean ADIP for reuse. The regenerator column has a temperature and pressure that are suitable for acid gas removal. When the rich ADIP enters the regenerator, the entrained acid gases are stripped. As the acid gases leaves the regenerator as overhead, any free water is removed to prevent acid formation. The acid gases are then sent to flare. The lean ADIP leaves the extractor bottom and is cooled and filtered. Lean ADIP returns to the last mixer/settler and flows back through the system in the counter-current direction of the propane to improve contact between the propane and ADIP, which improves H₂S and COS extraction.

C3/C4 MEROX Treating Section

MEROX treating removes mercaptan sulfur from C3/C4 product. Mercaptans are removed using a solution of sodium hydroxide (NaOH), also known by the commercial name caustic soda (hereinafter referred to as “caustic”) and MEROX. The MEROX catalyst facilitates the oxidation of mercaptans to disulfides. The oxidation takes place in an alkaline environment, which is provided by using the caustic solution. MEROX treating for C3 and C4 is similar. Both products are prewashed with caustic to remove any remaining traces of H₂S, COS, and CO₂. This prevents damage to the caustic that is used in MEROX treating. After prewashing, product flows to an extractor, where a caustic solution with MEROX catalyst contacts with the product. The caustic/catalyst solution converts the mercaptans into mercaptides. The sweetened product, which is lean on acid gases, leaves the extractor as overhead and any remaining caustic is separated. Caustic leaves the bottom of both product extractors rich with mercaptides. The rich caustic is regenerated into lean caustic for reuse. The C3/C4 extraction sections share a common caustic regeneration section, namely, an oxidizer. Before entering the bottom of the oxidizer, the rich caustic is injected with MEROX catalyst to maintain proper catalyst concentration, heated, and mixed with process air. In the oxidizer, the mercaptides are oxidized into disulfides. The mixture of disulfides, caustic, and air leave the oxidizer as overhead. The air, disulfide gases, and disulfide oil are separated from the regenerated caustic. The regenerated caustic is pumped to the C3/C4 extractor. Regenerated caustic with any residual disulfides is washed with NG in the NG wash settler.

C3/C4 Dehydration Section

Propane or butane products (or both) contain water when they leave MEROX treating. Dehydration removes moisture in such products through adsorption before the products flow to refrigeration and storage. The dehydration processes for C3 and C4 are similar. Both C3/C4 dehydration sections have two de-hydrators containing molecular sieve desiccant beds. One de-hydrator is in service while the other undergoes regeneration. Regeneration consists of heating the sieve beds to remove moisture, then cooling the beds before reuse. During drying, product flows up and through the molecular sieve bed, which adsorbs (that is, binds to its surface) moisture. From the top of the de-hydrator, dry C3/C4 products flow to refrigeration.

Natural Gasoline (NG) Processing Section

NG processing includes RVP control, de-colorizing and de-pentanizing sections.

RVP Control Section

A Reid vapor pressure (RVP) control section (or rerun unit) is a fractionator column that receives the C5+NG from the debutanizer bottom. The RVP control section collects a pentane product. The RVP control section can be used to adjust the RVP of the pentane product at a rerun fractionator overhead before the pentane product is sent to a pentane storage tank. RVP is a measure of the ability of a hydrocarbon to vaporize. RVP (sometimes called volatility) is an important specification in gasoline blending. The RVP control section stabilizes the RVP of NG by removing small amounts of pentane. Depending on operational requirements, the RVP control section can be totally or partially bypassed. NG from the debutanizer bottoms goes to the RVP column where a controlled amount of pentane is stripped and leaves the column as overhead gas. As in NGL fractionation, the overhead gas is condensed with coolers, and some of the condensate is pumped back to the column as reflux. The remaining pentane is cooled and sent to storage. If the RVP column bottoms product (NG) meets color specifications, it is sent to storage. If not, it is sent to decolorizing.

De-Colorizing Section

The de-colorizing section removes color bodies from NG. Color bodies are traces of heavy ends found in the de-butanizer bottoms product. Other impurities such as corrosion products from the pipeline may also be present. These must be removed for NG to meet the color specification. De-colorizer feed can be RVP column bottoms product or de-butanizer bottoms product, or a combination of both. Additional natural gasoline can also be supplied from other facilities to maintain a hexane plus (C6+) product supply. If de-colorizing is needed, NG first passes through a pre-flash-drum. A large portion of the lighter NG components vaporizes and leaves the drum as overhead. The heavier NG components remain along with the color bodies and are fed to the de-colorizer column, where the remaining color bodies are separated. The NG leaves the de-colorizer as overhead gas and is condensed and collected in the NG product drum, with some pumped back to the column as reflux. Overhead from the column and flash drum are joined and pumped to either the de-pentanizer (described later) or cooled and sent to storage in the feed product surge unit. The color bodies leave the de-colorizer as bottoms product and are pumped to the feed and surge unit to be injected into a crude line.

De-Pentanizing Section

De-pentanizing uses a fractionation column to produce a pentane overhead product and a C6+ bottoms product. Both the pentane product and the C6+ bottoms product are separately fed to storage or downstream the petrochemical plants. The feed to the de-pentanizer is the NG product stream from the de-colorizing section. Feed can be increased or decreased based on the demand for C6+ bottoms product. If the NGL fractionation plant NG production cannot meet demand, NG can be imported from oil refineries. The de-colorized NG is preheated before entering the de-pentanizer. The separated pentane leaves the column as overhead gas. The overhead condensers cool the overhead stream, and some is pumped back to the column as reflux. The remaining pentane is cooled and sent to storage. Light NG in the bottoms is vaporized and returned to heat the de-pentanizer. The remaining bottoms product is cooled and sent to storage as C6+.

Table 2 lists duty per train of major waste heat streams in an example of an NGL fractionation plant.

TABLE 2 Duty/train Stream Name (MMBtu/h) Propane refrigerant condenser 94 Propane de-hydration condenser 22 Butane de-hydrator condenser 9 Naphtha cooler 11 De-pentanizer condenser 100 ADIP cooler 73 Regenerator OVHD condenser 18 NG flash vapor condenser 107 NG de-colorizer condenser 53 Natural gasoline (cooling) process 29 propane condenser Fractionation propane condenser 81 Air cooled condenser 16 Regeneration gas cooler 22 RVP column condenser 36 Butane condenser 49 De-propanizer condenser 194 De-butanizer condenser 115

In Table 2, “Duty/train” represents each stream's thermal duty in millions Btu per hour (MMBtu/h) per processing train. A typical NGL fractionation plant includes three to four processing trains.

The systems described in this disclosure can be integrated with a NGL fractionation plant to make the fractionation plant more energy efficient or less polluting or both. In particular, the energy conversion system can be implemented to recover low grade waste heat from the NGL fractionation plant. Low grade waste heat is characterized by a temperature difference between a source and sink of the low grade heat steam being between 65° C. and 232° C. (150° F. and 450° F.). The NGL fractionation plant is an attractive option for integration with energy conversion systems due to a large amount of low grade waste heat generated by the plant and an absence of a need for deep cooling. Deep cooling refers to a temperature that is less than ambient that uses a refrigeration cycle to maintain.

The low grade waste heat from an NGL fractionation plant can be used for commodities such as carbon-free power generation, cooling capacity generation, potable water production from sea water, or combinations thereof. Low grade waste heat is characterized by a temperature ranging between 65° C. and 232° C. (150° F. to 450° F.). The waste heat can be used for the mono-generation, co-generation, or tri-generation of one or more or all of the commodities mentioned earlier. Low grade waste heat from the NGL fractionation plant can be used to provide in-plant sub-ambient cooling, thus reducing the consumption of power or fuel (or both) of the plant. Low grade waste heat from the NGL fractionation plant can be used to provide ambient air conditioning or cooling in the industrial community or in a nearby non-industrial community, thus helping the community to consume energy from alternative sources. In addition, the low grade waste heat can be used to desalinate water and produce potable water to the plant and adjacent community. An NGL fractionation plant is selected for low grade waste heat recovery because of a quantity of low grade waste heat available from the NGL fractionation plant as well as a cooling requirement of the plant to ambient temperature cooling (instead of deep cooling).

The energy conversion systems described in this disclosure can be integrated into an existing NGL fractionation plant as a retrofit or can be part of a newly constructed NGL fractionation plant. A retrofit to an existing NGL fractionation plant allows the carbon-free power generation, and fuel savings advantages offered by the energy conversion systems described here to be accessible with a reduced capital investment. For example, the energy conversion systems described here can produce one or more or all of substantially between 35 MW and 40 MW (for example, 37 MW) of carbon-free power, substantially between 100,000 and 150,000 m³/day (for example, 120,000 m³/day) of desalinated water, and substantially between 350 MM BTU/h and 400 MM BTU/h (for example, 388 MM BTU/h) of cooling capacity for in-plant or community utilization or both.

As described later, the systems for waste heat recovery and re-use from the NGL fractionation plant can include modified multi-effect distillation (MED) systems, customized Organic Rankine Cycle (ORC) systems, unique ammonia-water mixture Kalina cycle systems, customized modified Goswami cycle systems, mono-refrigerant specific vapor compression-ejector-expander triple cycle systems, or combinations of one or more of them. Details of each disclosure are described in the following paragraphs.

Heat Exchangers

In the configurations described in this disclosure, heat exchangers are used to transfer heat from one medium (for example, a stream flowing through a plant in a NGL fractionation plant, a buffer fluid or such medium) to another medium (for example, a buffer fluid or different stream flowing through a plant in the NGL fractionation plant). Heat exchangers are devices which transfer (exchange) heat typically from a hotter fluid stream to a relatively less hotter fluid stream. Heat exchangers can be used in heating and cooling applications, for example, in refrigerators, air conditions or such cooling applications. Heat exchangers can be distinguished from one another based on the direction in which fluids flow. For example, heat exchangers can be parallel-flow, cross-flow or counter-current. In parallel-flow heat exchangers, both fluid involved move in the same direction, entering and exiting the heat exchanger side-by-side. In cross-flow heat exchangers, the fluid path runs perpendicular to one another. In counter-current heat exchangers, the fluid paths flow in opposite directions, with one fluid exiting whether the other fluid enters. Counter-current heat exchangers are sometimes more effective than the other types of heat exchangers.

In addition to classifying heat exchangers based on fluid direction, heat exchangers can also be classified based on their construction. Some heat exchangers are constructed of multiple tubes. Some heat exchangers include plates with room for fluid to flow in between. Some heat exchangers enable heat exchange from liquid to liquid, while some heat exchangers enable heat exchange using other media.

Heat exchangers in a NGL fractionation plant are often shell and tube type heat exchangers which include multiple tubes through which fluid flows. The tubes are divided into two sets—the first set contains the fluid to be heated or cooled; the second set contains the fluid responsible for triggering the heat exchange, in other words, the fluid that either removes heat from the first set of tubes by absorbing and transmitting the heat away or warms the first set by transmitting its own heat to the fluid inside. When designing this type of exchanger, care must be taken in determining the correct tube wall thickness as well as tube diameter, to allow optimum heat exchange. In terms of flow, shell and tube heat exchangers can assume any of three flow path patterns.

Heat exchangers in NGL facilities can also be plate and frame type heat exchangers. Plate heat exchangers include thin plates joined together with a small amount of space in between, often maintained by a rubber gasket. The surface area is large, and the corners of each rectangular plate feature an opening through which fluid can flow between plates, extracting heat from the plates as it flows. The fluid channels themselves alternate hot and cold liquids, meaning that the heat exchangers can effectively cool as well as heat fluid. Because plate heat exchangers have large surface area, they can sometimes be more effective than shell and tube heat exchangers.

Other types of heat exchangers can include regenerative heat exchangers and adiabatic wheel heat exchangers. In a regenerative heat exchanger, the same fluid is passed along both sides of the exchanger, which can be either a plate heat exchanger or a shell and tube heat exchanger. Because the fluid can get very hot, the exiting fluid is used to warm the incoming fluid, maintaining a near constant temperature. Energy is saved in a regenerative heat exchanger because the process is cyclical, with almost all relative heat being transferred from the exiting fluid to the incoming fluid. To maintain a constant temperature, a small quantity of extra energy is needed to raise and lower the overall fluid temperature. In the adiabatic wheel heat exchanger, an intermediate liquid is used to store heat, which is then transferred to the opposite side of the heat exchanger. An adiabatic wheel consists of a large wheel with threads that rotate through the liquids—both hot and cold—to extract or transfer heat. The heat exchangers described in this disclosure can include any one of the heat exchangers described earlier, other heat exchangers, or combinations of them.

Each heat exchanger in each configuration can be associated with a respective thermal duty (or heat duty). The thermal duty of a heat exchanger can be defined as an amount of heat that can be transferred by the heat exchanger from the hot stream to the cold stream. The amount of heat can be calculated from the conditions and thermal properties of both the hot and cold streams. From the hot stream point of view, the thermal duty of the heat exchanger is the product of the hot stream flow rate, the hot stream specific heat, and a difference in temperature between the hot stream inlet temperature to the heat exchanger and the hot stream outlet temperature from the heat exchanger. From the cold stream point of view, the thermal duty of the heat exchanger is the product of the cold stream flow rate, the cold stream specific heat and a difference in temperature between the cold stream outlet from the heat exchanger and the cold stream inlet temperature from the heat exchanger. In several applications, the two quantities can be considered equal assuming no heat loss to the environment for these units, particularly, where the units are well insulated. The thermal duty of a heat exchanger can be measured in watts (W), megawatts (MW), millions of British Thermal Units per hour (Btu/hr), or millions of kilocalories per hour (Kcal/h). In the configurations described here, the thermal duties of the heat exchangers are provided as being “about X MW,” where “X” represents a numerical thermal duty value. The numerical thermal duty value is not absolute. That is, the actual thermal duty of a heat exchanger can be approximately equal to X, greater than X or less than X.

Flow Control System

In each of the configurations described later, process streams (also called “streams”) are flowed within each plant in a NGL fractionation plant and between plants in the NGL fractionation plant. The process streams can be flowed using one or more flow control systems implemented throughout the NGL fractionation plant. A flow control system can include one or more flow pumps to pump the process streams, one or more flow pipes through which the process streams are flowed and one or more valves to regulate the flow of streams through the pipes.

In some implementations, a flow control system can be operated manually. For example, an operator can set a flow rate for each pump and set valve open or close positions to regulate the flow of the process streams through the pipes in the flow control system. Once the operator has set the flow rates and the valve open or close positions for all flow control systems distributed across the NGL fractionation plant, the flow control system can flow the streams within a plant or between plants under constant flow conditions, for example, constant volumetric rate or such flow conditions. To change the flow conditions, the operator can manually operate the flow control system, for example, by changing the pump flow rate or the valve open or close position.

In some implementations, a flow control system can be operated automatically. For example, the flow control system can be connected to a computer system to operate the flow control system. The computer system can include a computer-readable medium storing instructions (such as flow control instructions and other instructions) executable by one or more processors to perform operations (such as flow control operations). An operator can set the flow rates and the valve open or close positions for all flow control systems distributed across the NGL fractionation plant using the computer system. In such implementations, the operator can manually change the flow conditions by providing inputs through the computer system. Also, in such implementations, the computer system can automatically (that is, without manual intervention) control one or more of the flow control systems, for example, using feedback systems implemented in one or more plants and connected to the computer system. For example, a sensor (such as a pressure sensor, temperature sensor or other sensor) can be connected to a pipe through which a process stream flows. The sensor can monitor and provide a flow condition (such as a pressure, temperature, or other flow condition) of the process stream to the computer system. In response to the flow condition exceeding a threshold (such as a threshold pressure value, a threshold temperature value, or other threshold value), the computer system can automatically perform operations. For example, if the pressure or temperature in the pipe exceeds the threshold pressure value or the threshold temperature value, respectively, the computer system can provide a signal to the pump to decrease a flow rate, a signal to open a valve to relieve the pressure, a signal to shut down process stream flow, or other signals.

In some examples, waste heat from a natural gas liquid fractionation plant can be recovered from a network of one or more heat exchangers located in the natural gas liquid fractionation plant. The waste heat recovered by the heat exchangers can be used to power a Kalina cycle based waste heat to cooling conversion plant. A Kalina cycle is an energy conversion system that uses a mixture of ammonia and water in a closed loop arrangement. For instance, the plant can produce at least about 350 MM Btu/h of sub-ambient cooling capacity, such as between about 350 MM Btu/h and about 450 MM Btu/h, such as about 350 MM Btu/h, about 400 MM Btu/h, or about 450 MM Btu/h.

FIG. 1A is a schematic diagram of an example of a low grade waste heat recovery system. The schematic includes a storage tank 501 to store buffer fluid of a 1st type, for example, oil, pressurized water, or such buffer fluid. The buffer fluid from the storage tank 501 is flowed to a heat exchanger network 599 which, in some implementations, can include 14 heat exchangers (for example, heat exchangers 502 a, 502 b, 502 c, 502 d, 502 e, 502 f, 502 g, 502 h, 502 i, 502 j, 502 k, 502 l, 502 m, 502 n,), which are described in detail later. The buffer fluid is flowed through the heat exchanger network 599 and heated by streams in the NGL fractionation plant (described later). As described later, the heated buffer fluid from the storage tank 501 is used to generate power and sub-ambient cooling capacity in a Kalina cycle system 505. The buffer fluid is then returned to the storage tank 501.

Referring to FIG. 1B, a Kalina cycle based plant 500 includes the storage tank 501 that stores buffer fluid 504, such as oil, water, an organic fluid, or another buffer fluid. The buffer fluid 504 is pumped from the storage tank 501 to the heat exchanger network 599 (FIG. 1A) including the heat exchangers 502 a-502 n by a buffer fluid circulation pump 503. For instance, the buffer fluid 504 in the storage tank 501 can be at a temperature of between about 110° F. and about 130° F., such as about 110° F., about 120° F., or about 130° F.

Individual streams of buffer fluid 504 a-504 n are heated in each of the heat exchangers 502 a-502 n by recovery of waste heat from process streams in the natural gas liquid fractionation plant. The heat exchangers 502 a-502 n can be configured such that they are parallel to one another in relation to the flow of the buffer fluid 504 a-504 n. The heated streams of buffer fluid 504 a-504 n are joined into a single header of hot buffer fluid 504 downstream of the heat exchangers 502 a-502 n. The hot buffer fluid 504 can be at a temperature of, for example, between about 190° F. and about 210° F., such as about 190° F., about 200° F., or about 210° F. The hot buffer fluid 504 can flow at a rate of between about 3500 kg/s and about 4500 kg/s, such as about 3500 kg/s, about 4000 kg/s, or about 4500 kg/s.

The heat from the hot buffer fluid 504 is used to heat a working fluid 506, such as an ammonia-water mixture, in a Kalina cycle 505, which is used to provide in-plant sub-ambient cooling. For instance, the plant 500 can produce at least about 350 MM Btu/h of sub-ambient cooling capacity, such as between about 350 MM Btu/h and about 450 MM Btu/h, such as about 350 MM Btu/h, about 400 MM Btu/h, or about 450 MM Btu/h. The cooling capacity produced by the Kalina cycle 505 can save power that would have been expended in mechanical refrigeration. For instance, use of the Kalina cycle 505 to provide in-plant sub-ambient cooling can avoid power consumption of at least about 40 MW of power, such as between about 40 MW and about 50 MW, such as about 40 MW, about 45 MW, or about 50 MW.

The Kalina cycle 505 includes a pump 507. The pump 507 can consume, for instance, between about 1 MW and about 2 MW of power, such as about 1 MW, about 1.5 MW, or about 2 MW. The pump 507 can pump the ammonia-water mixture 506 from a starting pressure of, for instance, between about 3.5 Bar and about 4.5 Bar, such as about 3.5 Bar, about 4 Bar, or about 4.5 Bar; to a higher pressure of, for instance, between about 11 Bar and about 12 Bar, such as about 11 Bar, about 11.5 Bar, or about 12 Bar. The pump 507 can be sized to receive the ammonia-water mixture 506 at a flow rate of between about 500 kg/s and about 1000 kg/s, such as about 500 kg/s, about 750 kg/s, or about 1000 kg/s.

The working fluid 506 can be a mixture of ammonia and water, for instance, between about 45% and about 55% ammonia, such as about 45%, about 50%, or about 55%; and between about 45% and about 55% water, such as about 45%, about 50%, or about 55%. The working fluid 506 is pumped by the pump 507 into a network of heat exchangers 508 a, 508 b, 508 d that together achieve partial evaporation of the working fluid 506 using heat from the buffer fluid 504, directly or indirectly. The heat exchangers are divided into two parallel branches: a first branch including the heat exchangers 508 a and 508 b, and the second branch including a heat exchanger 508 c and the heat exchanger 508 d. The working fluid 506 flowing along the two branches is heated and partially vaporized using between about 500 MM Btu/h and about 1500 MM Btu/h, such as about 500 MM Btu/h, about 1000 MM Btu/h, or about 1500 MM Btu/h, of waste heat collected by the buffer fluid; and using heat from a bottoms stream of a Kalina cycle separator (the liquid vapor separator 510, such as an ammonia-water separator).

The first branch of heat exchangers 508 a and 508 b is in a parallel configuration with the second branch of the heat exchangers 508 c and 508 d in relation to the flow of the working fluid. Within each branch, the two heat exchangers are arranged in series in relation to the flow of the working fluid 506, such that the heat exchanger 508 a is in series with the heat exchanger 508 b and the heat exchanger 508 c is in series with the heat exchanger 508 d. With respect to the flow of the buffer fluid 504, the heat exchanger 508 b is in a parallel configuration with the heat exchanger 508 d, and the parallel heat exchangers 508 b and 508 d are in series with the heat exchanger 508 a.

The heat exchangers 508 a can have a thermal duty of, for instance, between about 100 MM Btu/h and about 200 MM Btu/h, such as about 100 MM Btu/h, about 125 MM Btu/h, about 150 MM Btu/h, about 175 MM Btu/h, or about 200 MM Btu/h. The heat exchanger 508 b can have a thermal duty of, for instance, between about 400 MM Btu/h and about 500 MM Btu/h, such as about 400 MM Btu/h, about 425 MM Btu/h, about 450 MM Btu/h, about 475 MM Btu/h, about 500 MM Btu/h. The heat exchanger 508 c can have a thermal duty of, for instance, between about 150 MM Btu/h and about 250 MM Btu/h, such as about 150 MM Btu/h, about 175 MM Btu/h, about 200 MM Btu/h, about 225 MM Btu/h, or about 250 MM Btu/h. The heat exchanger 508 d can have a thermal duty of, for instance, between about 300 MM Btu/h and about 400 MM Btu/h, such as about 300 MM Btu/h, about 325 MM Btu/h, about 350 MM Btu/h, about 375 MM Btu/h, or about 400 MM Btu/h. The buffer fluid 504 flowing through the network of heat exchangers 508 a, 508 b, 508 d cools and returns to the storage tank 501.

The working fluid 506 exiting the pump 507 can have a temperature of, for instance, between about 80° F. and about 100° F., such as about 80° F., about 90° F., or about 100° F. The working fluid 506 from the pump 507 is split into two portions, for instance, with a split ratio of about between about 50% and about 54%, such as about 50%, about 52%, or about 54%.

A first portion 509 a of the working fluid 506 from the pump 507 is pre-heated and partially vaporized by exchange with the buffer fluid 504 in the heat exchangers 508 a and 508 b, which are in series in relation to the working fluid flow. For instance, the first portion 509 a of the working fluid 506 is heated to a temperature of between about 160° F. and about 180° F., such as about 160° F., about 170° F., or about 180° F.

A second portion 509 b of the working fluid 506 from the pump 507 is pre-heated and partially vaporized by exchange with a liquid stream 511 (from a liquid-vapor separator 510, described in the following paragraphs) in the heat exchanger 508 c. For instance, the second portion 509 b is heated to a temperature of between about 120° F. and about 140° F., such as about 120° F., about 130° F., or about 140° F. The heated second portion 509 b is further heated and partially vaporized by exchange with the buffer fluid 504 in the heat exchanger 508 d, which is in series in relation to the working fluid flow with the heat exchanger 508 c. For instance, the second portion 509 b is heated to a temperature of between about 160° F. and about 180° F., such as about 160° F., about 170° F., or about 180° F.

The first and second portions of the working fluid, which are heated and partially vaporized, flow into the liquid-vapor separator 510 that separates liquid from vapor, such as liquid ammonia and water from ammonia-water vapor. The pressure of the working fluid upon entry into the liquid-vapor separator 510 can be, for instance, between about 10 Bar and about 11 Bar, such as about 10 Bar, about 10.5 Bar, or about 11 Bar. A liquid stream 511 of the working fluid, such as liquid ammonia and water 511, which is a lean stream, exits the bottom of the separator 510 and a vapor stream 512 of the working fluid, such as ammonia-water vapor, exits the top of the separator 510.

The vapor stream 512, which is a rich stream, flows to a cooler 516, that condenses the stream 512 at high pressure. The condensed stream exiting the water cooler 516 is at a temperature of between about 70° F. and about 90° F., such as about 70° F., about 80° F., or about 90° F. The stream 512 is cooled in the water cooler 516 by exchange with a stream of cooling fluid 517, such as water, which is heated from a temperature of between about 70° F. and about 90° F., such as about 70° F., about 80° F., or about 90° F.; to a temperature of between about 80° F. and about 100° F., such as about 80° F., about 90° F., or about 100° F. The cooling fluid can flow through the heat exchanger at a rate of between about 15000 kg/s and about 20000 kg/s, such as about 15000 kg/s, about 16000 kg/s, about 17000 kg/s, about 18000 kg/s, about 19000 kg/s, or about 20000 kg/s. The cooler 516 can have a thermal duty of between about 400 MM Btu/h and about 600 MM Btu/h, such as about 400 MM Btu/h, about 500 MM Btu/h, or about 600 MM Btu/h.

The condensed stream 512 is throttled in a throttling valve 523 to a lower pressure of between about 4 Bar and about 5 Bar, such as about 4 Bar, about 4.5 Bar, or about 5 Bar, to generate cooling capacity. The stream 512 exiting the throttling valve 523 is at a temperature of between about 30° F. and about 50° F., such as about 30° F., about 40° F., or about 50° F., and is used for in-plant cooling in a deethanizer section of the natural gas liquid fractionation plant. For instance, the stream 512 is used in a process chiller 518 to cool a stream of ethane 519 from the deethanizer section, such as a top stream of ethane gas from a deethanizer. The ethane 519 is cooled from a temperature of between about 45° F. and about 55° F., such as about 45° F., about 50° F., or about 55° F.; to a temperature of between about 40° F. and about 50° F., such as about 40° F., about 45° F., or about 50° F. The stream 512 can be heated to a temperature of between about 35° F. and about 45° F., such as about 35° F., about 40° F., or about 45° F. The process chiller 518 can have a thermal duty of between about 300 MM Btu/h and about 500 MM Btu/h, such as about 300 MM Btu/h, about 400 MM Btu/h, or about 500 MM Btu/h. The ethane 519 can flow through the process chiller 518 at a flow rate of between about 600 kg/s and about 800 kg/s, such as about 600 kg/s, about 700 kg/s, or about 800 kg/s.

The liquid stream 511 flows via the heat exchanger 508 c to a high pressure recovery turbine (HPRT) 514, for example, a hydraulic liquid turbine, for power generation. After exchange at the heat exchanger 508 c, the temperature of the stream 511 is between about 130° F. and about 150° F., such as about 130° F., about 140° F., or about 150° F. The HPRT 514 can generate at least about 0.1 MW of power, such as between about 0.1 MW and about 0.5 MW of power, such as about 0.1 MW, about 0.25 MW, or about 0.5 MW of power. Power is generated by the HPRT 514 using a flow rate of the liquid stream 511 of between about 500 kg/s and about 1000 kg/s, such as about 500 kg/s, about 750 kg/s, or about 1000 kg/s. The HPRT 514 reduces the pressure of the liquid stream 511 to, for instance, between about 4 Bar and about 5 Bar, such as about 4 Bar, about 4.5 Bar, or about 5 Bar; and reduces the temperature of the liquid stream 511 to, for instance, between about 110° F. and about 130° F., such as about 110° F., about 120° F., or about 130° F.

The stream 512 and the stream 511 combine into a single stream of the working fluid 506 after exiting the turbine 514 and the chiller 516. The working fluid 506 is cooled in a cooler 515, such as a cooling water condenser or an air cooler, by exchange with cooling water. The cooler 515 can have a thermal duty of, for example, between about 800 MM Btu/h and about 1000 MM Btu/h, such as about 800 MM Btu/h, about 900 MM Btu/h, or about 1000 MM Btu/h. The cooler 515 cools the working fluid 506 to a temperature of, for example, between about 80° F. and about 100° F., such as about 80° F., about 90° F., or about 100° F. The cooling water used to cool the working fluid 506 can have a temperature of between about 70° F. and about 90° F., such as about 70° F., about 80° F., or about 90° F.; and can be heated to a temperature of between about 80° F. and about 100° F., such as about 80° F., about 90° F., or about 100° F. In some examples, the temperature of the cooling water can vary depending on the season. For instance, the cooling water can have a lower temperature in winter than in summer. The volume of cooling water flowing through the cooler 515 can be between about 9000 kg/s and about 11000 kg/s, such as about 9000 kg/s, about 10000 kg/s, or about 11000 kg/s.

In the system 500 of FIG. 1B, the buffer fluid 504 provides between about 900 MM Btu/h and about 1000 MM Btu/h of energy through the heat exchangers 508 a, 508 b, 508 d. The ethane stream 519 provides between about 350 MM Btu/h and about 450 MM Btu/h of energy through the process chiller 518. In addition, net pumping converted to input energy, assuming approximately 65% efficiency, provides between about 3 MM Btu/h and about 8 MM Btu/h of energy. In total, the system 500 provides between about 1300 MM Btu/h and about 1400 MM Btu/h of energy.

Using a Kalina cycle for waste heat to cooling conversion can offer advantages. A Kalina cycle offers a degree of freedom in that the composition of the working fluid can be adjusted. This degree of freedom allows a Kalina cycle to be adapted to particular operating conditions, for example, to a particular heat source or a particular cooling fluid, in order to improve or optimize energy conversion and heat transfer. Furthermore, because ammonia has a similar molecular weight as water, ammonia-water vapor as a working fluid behaves similarly to steam, thus permitting the use of standard steam turbine components. At the same time, the use of a binary fluid allows the composition of the fluid to be varied throughout the cycle, for example, to provide a richer composition at the evaporator and a leaner composition at the condenser. In addition, ammonia is an environmentally friendly compound that is less hazardous than compounds, such as iso-butane, that are often used in other power conversion cycles.

The heat exchangers 502 a-502 n can be incorporated into various sections of a natural gas liquid fractionation plant to recover waste heat from liquid or vapor streams in those sections.

Referring to FIG. 1C, in a propane dehydrator section of a natural gas liquid fractionation plant, wet propane 531 is dehydrated in a propane dehydrator 532. The wet propane 531 can be, for instance, propane gas from a depropanizer section of the natural gas liquid fractionation plant. A portion 533 of the dry propane from the propane dehydrator 532 is output as dry propane, for instance, to a propane refrigeration section (FIG. 1J). Another portion 534 of the propane from the propane dehydrator 532 is further dehydrated in a propane dehydrator 536. The dry propane 534 output from the propane dehydrator 532 is cooled in the heat exchanger 502 a by exchange with the stream 504 a of buffer fluid. The cooled dry propane 534 is returned to a depropanizer reflux drum. The presence of the heat exchanger 502 a recovers waste heat from the dry propane 534, enabling other components (for instance, cooling units or condensers) that would have been used to cool the dry propane 534 to be bypassed or eliminated from the propane dehydrator section.

The stream 504 a of buffer fluid can be heated from a temperature of between about 115° F. and about 125° F. to a temperature of between about 390° F. and about 410° F., such as about 390° F., about 395° F., about 400° F., or about 410° F. The thermal duty of the heat exchanger 502 a can be between about 50 MM Btu/h and about 150 MM Btu/h, such as about 50 MM Btu/h, about 75 MM Btu/h, about 100 MM Btu/h, about 125 MM Btu/h, or about 150 MM Btu/h.

Referring to FIG. 1D, in a debutanizer section of the natural gas liquid fractionation plant, C4+ NGL bottoms product 528 from a depropanizer in a depropanizer section of the natural gas liquid fractionation plant are received into a debutanizer 535. A bottoms stream from the debutanizer 535 is processed in a reboiler 537, for instance, with heat provided by steam. Liquid butane from the reboiler is returned to the debutanizer 535. A C5+ bottoms product 538 from the debutanizer 535 is cooled in the heat exchanger 502 b by exchange with the stream 504 b of buffer fluid. The cooled C5+ bottoms product 538 is provided to a rerun unit (FIG. 1M). The presence of the heat exchanger 502 b recovers waste heat from the C5+ bottoms product 538, enabling other components (for instance, a naphtha cooling unit) that would have been used to cool the C5+ bottoms product 538 to be bypassed or eliminated from the debutanizer section.

The stream 504 b of buffer fluid can be heated from a temperature of between about 115° F. and about 125° F. to a temperature of between about 250° F. and about 270° F., such as about 250° F., about 260° F., about 261° F. or about 270° F. The thermal duty of the heat exchanger 502 b can be between about 25 MM Btu/h and about 125 MM Btu/h, such as about 25 MM Btu/h, about 50 MM Btu/h, about 75 MM Btu/h, about 100 MM Btu/h, or about 125 MM Btu/h.

Butane gas 539 exits from the top of the debutanizer 535 and is split into a first portion 539 a and a second portion 539 b. The first portion 539 a of the butane gas is cooled in the heat exchanger 502 c by exchange with the stream 504 c of buffer fluid. The second portion 539 b of the butane gas is cooled in an air cooler 529. The cooled portions 539 a, 539 b are combined into a single stream of cooled butane gas 539 that is collected in a reflux drum 540. A portion of the liquid butane from the reflux drum is returned to the debutanizer 535, and a portion of the liquid butane from the reflux drum 540 is either treated (for instance, in a MEROX unit) or sent to users as untreated product. The presence of the heat exchanger 502 c recovers waste heat from the butane gas 539, enabling other components (for instance, cooling units or condensers) that would have been used to cool the butane gas 539 to be bypassed or eliminated from the debutanizer section.

The stream 504 c of buffer fluid can be heated from a temperature of between about 115° F. and about 125° F. to a temperature of between about 140° F. and about 160° F., such as about 140° F., about 150° F., about 152° F. or about 160° F. The thermal duty of the heat exchanger 502 c can be between about 10 MM Btu/h and about 90 MM Btu/h, such as about 10 MM Btu/h, about 30 MM Btu/h, about 50 MM Btu/h, about 70 MM Btu/h, or about 80 MM Btu/h.

Referring to FIG. 1E, in a butane dehydrator section, wet butane 541 is dehydrated in a dehydrator 542. The wet butane 541 can include, for instance, the butane gas 539 in the debutanizer section (FIG. 1D). A portion of the dry butane 543 from the dehydrator 542 is output, for instance, to a butane refrigeration section of the natural gas liquid fractionation plant. Another portion 544 of the butane from the dehydrator 542 is further dehydrated in a butane dehydrator 545. The dry butane 544 output from the butane dehydrator 542 is cooled in the heat exchanger 502 d by exchange with the stream 504 d of buffer fluid. The cooled dry butane 544 is returned to the debutanizer reflux drum 540 (FIG. 1D). The presence of the heat exchanger 502 d recovers waste heat from the dry butane 544, enabling other components (for instance, cooling units or condensers) that would have been used to cool the dry butane 544 to be bypassed or eliminated from the butane dehydrator section.

The stream 504 d of buffer fluid can be heated from a temperature of between about 115° F. and about 125° F. to a temperature of between about 390° F. and about 410° F., such as about 390° F., about 395° F., about 400°, or about 410° F. The thermal duty of the heat exchanger 502 d can be between about 25 MM Btu/h and about 125 MM Btu/h, such as about 25 MM Btu/h, about 50 MM Btu/h, about 75 MM Btu/h, about 100 MM Btu/h, or about 125 MM Btu/h.

Referring to FIG. 1F, in a depentanizer section of the natural gas liquid fractionation plant, a stream of C5+ NGL 547 received from a decolorizing section (FIG. 1H) is preheated in a heat exchanger 548 and provided into a depentanizer 549. A bottoms stream from the depentanizer 549 is processed in a reboiler 551, for instance, with heat provided by steam. Liquid pentane from the reboiler is returned to the depentanizer 549 and C6+ NGL bottoms 550 from the depentanizer 549 are used to heat the stream of C5+ NGL 547 in the heat exchanger 548 and then output to storage, such as to a surge spheroid.

A top stream 552 of pentane gas from the depentanizer 549 is cooled in the heat exchanger 502 e by exchange with the stream 504 e of buffer fluid. The cooled pentane 552 is collected in a reflux drum 553. A portion of the liquid pentane from the reflux drum 553 is returned to the depentanizer 549, and a portion of the liquid pentane from the reflux drum 553 is sent to storage, for instance, in a petrochemical plant. The presence of the heat exchanger 502 e recovers waste heat from the pentane gas 552, and enables other components (for instance, cooling units or condensers) that would have been used to cool the pentane gas 552 to be bypassed or eliminated from the depentanizer section.

The stream 504 e of buffer fluid can be heated from a temperature of between about 115° F. and about 125° F. to a temperature of between about 160° F. and about 180° F., such as about 160° F., about 165° F., about 170° F., or about 180° F. The thermal duty of the heat exchanger 502 e can be between about 50 MM Btu/h and about 150 MM Btu/h, such as about 50 MM Btu/h, about 75 MM Btu/h, about 100 MM Btu/h, or about 125 MM Btu/h, or about 150 MM Btu/h.

Referring to FIG. 1G, in a solvent regeneration section, rich ADIP 554 from an ADIP extractor (not shown) is fed into an ADIP generator 555 to be regenerated into lean ADIP for reuse. Acid gases 556 leave the top of the ADIP generator 555 and are cooled in the heat exchanger 502 f by exchange with the stream 504 f of buffer fluid. The cooled acid gases 556 are refluxed in a reflux drum 557. Acid gas 558 from the reflux drum 557 is sent to flare and any remaining ADIP is returned to the ADIP generator 555. The presence of the heat exchanger 502 f recovers waste heat from the acid gases 556, enabling other components (for instance, cooling units or condensers) that would have been used to cool the acid gases 556 to be bypassed or eliminated from the solvent regeneration section.

The stream 504 f of buffer fluid can be heated from a temperature of between about 115° F. and about 125° F. to a temperature of between about 220° F. and about 240° F., such as about 220° F., about 227° F., about 230° F., or about 240° F. The thermal duty of the heat exchanger 502 f can be between about 10 MM Btu/h and about 90 MM Btu/h, such as about 10 MM Btu/h, about 30 MM Btu/h, about 50 MM Btu/h, about 70 MM Btu/h, or about 90 MM Btu/h.

Lean ADIP 559 leaves the bottom of the ADIP generator 555 and is cooled in the heat exchanger 502 g by exchange with the stream 504 g of buffer fluid. The cooled lean ADIP 559 is returned to the ADIP extractor. The presence of the heat exchanger 502 g recovers waste heat from the lean ADIP 559, enabling other components (for instance, cooling units or condensers) that would have been used to cool the lean ADIP 559 to be bypassed or eliminated from the solvent regeneration section.

The stream 504 g of buffer fluid can be heated from a temperature of between about 115° F. and about 125° F. to a temperature of between about 160° F. and about 180° F., such as about 160° F., about 170° F., about 171° F., or about 180° F. The thermal duty of the heat exchanger 502 g can be between about 150 MM Btu/h and about 250 MM Btu/h, such as about 150 MM Btu/h, about 175 MM Btu/h, about 200 MM Btu/h, about 225 MM Btu/h, or about 250 MM Btu/h.

Referring to FIG. 1H, in a decolorizing section of the natural gas liquid fractionation plant, NG 560 from the rerun unit is processed in a pre-flash drum 561. Light NG components 562 exit from the pre-flash drum 561 as overhead and are cooled in the heat exchanger 502 h by exchange with the stream 504 h of buffer fluid. The cooled light NG components 562 are stored in a product drum 563. The presence of the heat exchanger 502 h recovers waste heat from the light NG components 562, enabling other components (for instance, cooling units or condensers) that would have been used to cool the light NG components 562 to be bypassed or eliminated from the decolorizing section.

The stream 504 h of buffer fluid can be heated from a temperature of between about 115° F. and about 125° F. to a temperature of between about 200° F. and about 220° F., such as about 200° F., about 210° F., about 211° F., or about 220° F. The thermal duty of the heat exchanger 502 h can be between about 50 MM Btu/h and about 150 MM Btu/h, such as about 50 MM Btu/h, about 75 MM Btu/h, about 100 MM Btu/h, about 125 MM Btu/h, or about 150 MM Btu/h.

Heavy NG components and color bodies exit from the pre-flash drum 561 as a bottoms stream 564 and are fed into a decolorizer 565. Color bodies leave the bottom of the decolorizer 565 and are pumped to a feed and surge unit to be injected into a crude line. NG leaves the decolorizer 565 as overhead NG gas 566, which is cooled in the heat exchanger 502 i by exchange with the stream 504 i of buffer fluid. The cooled NG gas 566 is provided to a reflux drum 567. A portion of the liquid NG from the reflux drum 567 is stored in the product drum 563 and a portion is returned to the decolorizer 565. The presence of the heat exchanger 502 i recovers waste heat from the NG gas 566, enabling other components (for instance, cooling units or condensers) that would have been used to cool the NG gas 566 to be bypassed or eliminated from the decolorizing section.

The stream 504 i of buffer fluid can be heated from a temperature of between about 115° F. and about 125° F. to a temperature of between about 220° F. and about 240° F., such as about 220° F., about 229° F., about 230° F., or about 240° F. The thermal duty of the heat exchanger 502 i can be between about 25 MM Btu/h and about 125 MM Btu/h, such as about 25 MM Btu/h, about 50 MM Btu/h, about 75 MM Btu/h, about 100 MM Btu/h, or about 125 MM Btu/h.

Referring to FIG. 11I, in a propane vapor recovery unit, propane 568 is received into a flash drum 569. A bottoms product of liquid propane is sent to propane storage. An overhead product 570 of propane vapor is compressed in a compressor 571 and cooled in the heat exchanger 502 j by exchange with the stream 504 j of buffer fluid. The cooled propane 570 is stored in a product drum 572 and returned to the flash drum 569. The presence of the heat exchanger 502 j recovers waste heat from the propane vapor 570, enabling other components (for instance, cooling units or condensers) that would have been used to cool the propane vapor 570 to be bypassed or eliminated from the vapor recovery unit.

The stream 504 j of buffer fluid can be heated from a temperature of between about 115° F. and about 125° F. to a temperature of between about 250° F. and about 270° F., such as about 250° F., about 260° F., about 263° F., or about 270° F. The thermal duty of the heat exchanger 502 j can be between about 10 MM Btu/h and about 90 MM Btu/h, such as about 10 MM Btu/h, about 30 MM Btu/h, about 50 MM Btu/h, about 70 MM Btu/h, or about 90 MM Btu/h.

Referring to FIG. 1J, in a propane refrigeration section, dry propane 532 from the propane dehydration section (FIG. 1C) is compressed in a compressor 573. The compressed dry propane 532 from the compressor 573 is cooled in the heat exchanger 502 k by exchange with the stream 504 k of buffer fluid. The cooled dry propane 532 is stored in a propane receiver 574. The presence of the heat exchanger 502 k recovers waste heat from the dry propane 532, enabling other components (for instance, cooling units or condensers) that would have been used to cool the dry propane 532 to be bypassed or eliminated from the propane refrigeration section.

The stream 504 k of buffer fluid can be heated from a temperature of between about 115° F. and about 125° F. to a temperature of between about 190° F. and about 210° F., such as about 190° F., about 192° F., about 200° F., or about 210° F. The thermal duty of the heat exchanger 502 k can be between about 50 MM Btu/h and about 150 MM Btu/h, such as about 50 MM Btu/h, about 75 MM Btu/h, about 100 MM Btu/h, about 125 MM Btu/h, or about 150 MM Btu/h.

Referring to FIG. 1K, in some examples, propane product 577 can be sub-cooled in a propane product sub-cooling section by exchange in a propane chiller 575 with a cooling fluid 576. After cooling the propane product 574 in the propane chiller 575, the cooling fluid 576 is compressed and cooled in the heat exchanger 502 l by exchange with the stream 504 l of buffer fluid. The cooled cooling fluid 576 is returned to the propane chiller 575 for further propane cooling. The presence of the heat exchanger 502 l recovers waste heat from the cooling fluid 576, enabling other components (for instance, cooling units or condensers) that would have been used to cool the cooling fluid 576 to be bypassed or eliminated from the propane product sub-cooling section.

The stream 504 l of buffer fluid can be heated from a temperature of between about 115° F. and about 125° F. to a temperature of between about 230° F. and about 250° F., such as about 230° F., about 237° F., about 240° F., or about 250° F. The thermal duty of the heat exchanger 502 l can be between about 25 MM Btu/h and about 125 MM Btu/h, such as about 25 MM Btu/h, about 50 MM Btu/h, about 75 MM Btu/h, about 100 MM Btu/h, or about 125 MM Btu/h.

Referring to FIG. 1L, in an ethane production section, ethane 582 is dried in a dryer 583 operating in a regeneration mode and cooled in the heat exchanger 502 m by exchange with the stream 504 m of buffer fluid. The cooled ethane 582 is separated in a feed gas separator 584 and ethane vapor 585 is further dried in a dryer 586 operating in a drying mode. Water is removed. Dry ethane output from the dryer 586 is heated and send to a sales gas grid or elsewhere. The presence of the heat exchanger 502 m recovers waste heat from the ethane 582, enabling other components (for instance, cooling units or condensers) that would have been used to cool the ethane 582 to be bypassed or eliminated from the ethane production section.

The stream 504 m of buffer fluid can be heated from a temperature of between about 115° F. and about 125° F. to a temperature of between about 400° F. and about 420° F., such as about 400° F., about 410° F., or about 420° F. The thermal duty of the heat exchanger 502 m can be between about 10 MM Btu/h and about 90 MM Btu/h, such as about 10 MM Btu/h, about 30 MM Btu/h, about 50 MM Btu/h, about 70 MM Btu/h, or about 90 MM Btu/h.

Referring to FIG. 1M, in an NG vapor pressure control section, debutanizer bottoms 538 from the debutanizer 535 (FIG. 1D) are received into an RVP column 587. An overhead stream of pentane 588 leaves the RVP column and is cooled in the heat exchanger 502 n by exchange with the stream 504 n of buffer fluid. The cooled pentane 588 is provided to a reflux drum 589. A portion of the liquid pentane from the reflux drum 589 is returned to the RVP column 587 and a portion is sent to storage. The presence of the heat exchanger 502 n recovers waste heat from the pentane 588, enabling other components (for instance, cooling units or condensers) that would have been used to cool the pentane 588 to be bypassed or eliminated from the NG vapor pressure control section.

The stream 504 n of buffer fluid can be heated from a temperature of between about 115° F. and about 125° F. to a temperature of between about 200° F. and about 220° F., such as about 200° F., about 210° F., about 211° F. or about 220° F. The thermal duty of the heat exchanger 502 n can be between about 10 MM Btu/h and about 90 MM Btu/h, such as about 10 MM Btu/h, about 30 MM Btu/h, about 50 MM Btu/h, about 70 MM Btu/h, or about 90 MM Btu/h.

The systems described here can enable low-grade waste heat from the NGL fractionation plant to be used for carbon-free generation of cooling capacity, enabling the NGL fractionation plant to be more energy efficient, less polluting, or both.

The network of heat exchangers described here can be integrated into an existing NGL fractionation plant as a retrofit or can be integrated into a newly constructed NGL fractionation plant. A retrofit to an existing NGL fractionation plant allows the efficiency, cooling capacity, and fuel savings offered by the energy conversion systems described here to be accessible with a relatively low-capital investment. The energy conversion systems can make use of existing structure in an NGL fractionation plant while still enabling efficient waste heat recovery and conversion of waste heat to cooling capacity. The integration of an energy conversion system into an existing NGL fractionation plant can be generalizable to plant-specific operating modes.

Thus, particular implementations of the subject matter have been described. Other implementations are within the scope of the following claims. 

1. A system comprising: a waste heat recovery heat exchanger configured to heat a buffer fluid stream by exchange with a heat source in a natural gas liquid fractionation plant; a Kalina cycle energy conversion system including: one or more first energy conversion heat exchangers configured to heat a first portion of a working fluid by exchange with the heated buffer fluid stream; a separator configured to receive the heated working fluid and to output a vapor stream of the working fluid and the liquid stream of the working fluid; and a cooling subsystem including a first cooling element configured to condense the vapor stream of the working fluid and a second cooling element configured to cool a process fluid stream from the natural gas liquid fractionation plant by exchange with the condensed vapor stream of the working fluid.
 2. The system of claim 1, wherein the cooling subsystem is configured to produce at least 350 MM Btu/h of cooling capacity for the natural gas liquid fractionation plant.
 3. The system of claim 1, wherein the second cooling element is configured to cool ethane gas output from a deethanizer in the natural gas liquid fractionation plant.
 4. The system of claim 1, wherein the second cooling element comprises a chiller having a thermal duty of between 300 MM Btu/h and 500 MM Btu/h.
 5. The system of claim 1, wherein the first cooling element comprises a cooler having a thermal duty of between 400 Btu/h and 600 Btu/h.
 6. The system of claim 1, wherein the first cooling element comprises a valve.
 7. The system of claim 1, wherein the valve is configured to condense the working fluid to a pressure of between 4 Bar and 5 Bar and a temperature of between 30° F. and 50° F.
 8. The system of claim 1, wherein the energy conversion system comprises a pump configured to pump the working fluid to a pressure of between 11 Bar and 12 Bar.
 9. The system of claim 1, wherein the one or more first energy conversion heat exchangers comprise: an energy conversion heat exchanger having a thermal duty of between 100 MM Btu/h and 200 MM Btu/h; and an energy conversion heat exchanger having a thermal duty of between 400 MM Btu/h and about 500 MM Btu/h.
 10. The system of claim 1, wherein the one or more first energy conversion heat exchangers are configured to heat the first portion of the working fluid to a temperature of between 160° F. and 180° F.
 11. The system of claim 1, wherein the one or more first energy conversion heat exchangers are configured to heat a first portion of the working fluid, and wherein the Kalina cycle energy conversion system comprises one or more second energy conversion heat exchangers configured to heat a second portion of the working fluid, the second by exchange with the liquid stream of the working fluid.
 12. The system of claim 11, wherein the separator is configured to receive the heated first and second portions of the working fluid.
 13. The system of claim 11, wherein the one or more second energy conversion heat exchangers are configured to heat the second portion of the working fluid by exchange with the heated buffer fluid stream.
 14. The system of claim 11, wherein the one or more second energy conversion heat exchangers comprise: a heat exchanger having a thermal duty of between 150 MM Btu/h and 250 MM Btu/h; and a heat exchanger having a thermal duty of between 300 MM Btu/h and about 400 MM Btu/h.
 15. The system of claim 11, wherein the one or more second energy conversion heat exchangers are configured to heat the second portion of the working fluid to a temperature of between 160° F. and 180° F.
 16. The system of claim 1, comprising a turbine configured to generate power from the liquid stream of the working fluid.
 17. The system of claim 16, wherein the second turbine is configured to generate at least 0.1 MW of power.
 18. The system of claim 16, wherein the second turbine comprises a high pressure recovery turbine.
 19. The system of claim 1, comprising a storage tank, wherein the buffer fluid stream flows from the storage tank, through the waste heat recovery heat exchanger, through the Kalina cycle energy conversion system, and back to the storage tank.
 20. The system of claim 1, wherein the waste heat recovery heat exchanger is configured to heat the buffer fluid stream by exchange with propane gas output from a propane dehydrator in the natural gas liquid fractionation plant.
 21. The system of claim 1, wherein the waste heat recovery heat exchanger is configured to heat the buffer fluid stream by exchange with a C5+ bottoms product from a debutanizer in the natural gas liquid fractionation plant.
 22. The system of claim 1, wherein the waste heat recovery heat exchanger is configured to heat the buffer fluid stream by exchange with butane gas output from a debutanizer in the natural gas liquid fractionation plant.
 23. The system of claim 1, wherein the waste heat recovery heat exchanger is configured to heat the buffer fluid stream by exchange with butane gas output from a butane dehydrator in the natural gas liquid fractionation plant.
 24. The system of claim 1, wherein the waste heat recovery heat exchanger is configured to heat the buffer fluid stream by exchange with pentane gas output from a depentanizer in the natural gas liquid fractionation plant.
 25. The system of claim 1, wherein the waste heat recovery exchanger is configured to heat the buffer fluid stream by exchange with acid gases output from an ADIP generator in the natural gas liquid fractionation plant.
 26. The system of claim 1, wherein the waste heat recovery exchanger is configured to heat the buffer fluid stream by exchange with lean ADIP output from an ADIP generator in the natural gas liquid fractionation plant.
 27. The system of claim 1, wherein the waste heat recovery exchanger is configured to heat the buffer fluid stream by exchange with light NG components output from a pre-flash drum in a decolorizing section of the natural gas liquid fractionation plant.
 28. The system of claim 1, wherein the waste heat recovery exchanger is configured to heat the buffer fluid stream by exchange with NG gas output from a decolorizer in the natural gas liquid fractionation plant.
 29. The system of claim 1, wherein the waste heat recovery exchanger is configured to heat the buffer fluid stream by exchange with compressed propane in the natural gas liquid fractionation plant.
 30. The system of claim 1, wherein the waste heat recovery exchanger is configured to heat the buffer fluid stream by exchange with dry ethane gas in the natural gas liquid fractionation plant.
 31. The system of claim 1, wherein the waste heat recovery exchanger is configured to heat the buffer fluid stream by exchange with pentane gas output from an RVP column in the natural gas liquid fractionation plant.
 32. A method comprising: heating a buffer fluid stream via a waste heat recovery heat exchanger by exchange with a heat source in a natural gas liquid fractionation plant; generating power in a Kalina cycle energy conversion system, comprising: heating a working fluid via one or more first energy conversion heat exchangers by exchange with the heated buffer fluid stream; separating, in a separator, the heated working fluid into a vapor stream of the working fluid and the liquid stream of the working fluid; condensing the vapor stream of the working fluid; and cooling a process fluid stream in the natural gas liquid fractionation plant by exchange with the condensed vapor stream of the working fluid.
 33. The method of claim 32, wherein cooling the process fluid stream comprises producing at least 350 MM Btu/h of cooling capacity for the natural gas liquid fractionation plant.
 34. The method of claim 32, wherein cooling the process fluid stream comprises cooling ethane gas output from a deethanizer in the natural gas liquid fractionation plant.
 35. The method of claim 32, comprising pumping the working fluid to a pressure of between 11 Bar and 12 Bar.
 36. The method of claim 32, wherein heating the working fluid comprises heating the working fluid to a temperature of between 160° F. and 180° F.
 37. The method of claim 32, wherein heating the working fluid comprises heating a first portion of the working fluid by exchange with the heated buffer fluid, and comprising heating a second portion of the working fluid via one or more second energy conversion heat exchangers by exchange with the liquid stream of the working fluid.
 38. The method of claim 32, comprising generating power from the liquid stream of the working fluid by a second turbine.
 39. The method of claim 32, comprising flowing the buffer fluid stream from a storage tank, through the waste heat recovery exchanger, through the Kalina cycle energy conversion system, and back to the storage tank.
 40. The method of claim 32, wherein heating the buffer fluid stream comprises heating the buffer fluid stream by exchange with propane gas output from a propane dehydrator in the natural gas liquid fractionation plant.
 41. The method of claim 32, wherein heating the buffer fluid stream comprises heating the buffer fluid stream by exchange with a C5+ bottoms product from a debutanizer in the natural gas liquid fractionation plant.
 42. The method of claim 32, wherein heating the buffer fluid stream comprises heating the buffer fluid stream by exchange with butane gas output from a debutanizer in the natural gas liquid fractionation plant.
 43. The method of claim 32, wherein heating the buffer fluid stream comprises heating the buffer fluid stream by exchange with butane gas output from a butane dehydrator in the natural gas liquid fractionation plant.
 44. The method of claim 32, wherein heating the buffer fluid stream comprises heating the buffer fluid stream by exchange with pentane gas output from a depentanizer in the natural gas liquid fractionation plant.
 45. The method of claim 32, wherein heating the buffer fluid stream comprises heating the buffer fluid stream by exchange with acid gases output from an ADIP generator in the natural gas liquid fractionation plant.
 46. The method of claim 32, wherein heating the buffer fluid stream comprises heating the buffer fluid stream by exchange with lean ADIP output from an ADIP generator in the natural gas liquid fractionation plant.
 47. The method of claim 32, wherein heating the buffer fluid stream comprises heating the buffer fluid stream by exchange with light NG components output from a pre-flash drum in a decolorizing section of the natural gas liquid fractionation plant.
 48. The method of claim 32, wherein heating the buffer fluid stream comprises heating the buffer fluid stream by exchange with NG gas output from a decolorizer in the natural gas liquid fractionation plant.
 49. The method of claim 32, wherein heating the buffer fluid stream comprises heating the buffer fluid stream by exchange with compressed propane in the natural gas liquid fractionation plant.
 50. The method of claim 32, wherein heating the buffer fluid stream comprises heating the buffer fluid stream by exchange with dry ethane gas in the natural gas liquid fractionation plant.
 51. The method of claim 32, wherein heating the buffer fluid stream comprises heating the buffer fluid stream by exchange with pentane gas output from an RVP column in the natural gas liquid fractionation plant. 